CN104534812B - One is applied to gas cryogenic separation equipment main distillation column - Google Patents
One is applied to gas cryogenic separation equipment main distillation column Download PDFInfo
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- CN104534812B CN104534812B CN201510001527.0A CN201510001527A CN104534812B CN 104534812 B CN104534812 B CN 104534812B CN 201510001527 A CN201510001527 A CN 201510001527A CN 104534812 B CN104534812 B CN 104534812B
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Abstract
One is applied to gas cryogenic separation equipment main distillation column, and it relates to a kind of main distillation column.This device includes: take out pipe, lower tower liquid nitrogen reflux pipe, low pressure heat exchanger, boiling section, heat exchanger and main condenser vaporizer in rectifying column main body, two pressure nitrogen gas towers.The present invention affects air separation unit according to pressure tower nitrogen withdrawal amount under space division main distillation column and runs the technical Analysis of cold factor, for pressure nitrogen gas taken amount deficiency problem, proposition solution: 1) the taking-up mouth of pipe is increased away from gas-liquid boiling section, reduce droplet entrainment；2) change singly take out mouth as black soy sauce mouth minimizing exit velocity into.Reaching the stable adjustment of space division rectification operating mode after engineered, operational factor meets design load, reduces the tower fluctuation impact on ar system under main distillation column, eliminates low pressure heat exchanger low temperature stress fatigue and strength failure, add the purpose of the yield of pressure nitrogen gas.
Description
Technical field
The present invention relates to a kind of main distillation column.
Background technology
Aqueous vapor subsidiary factory of China Coal Longhua, Harbin Coal Chemical Industry Co., Ltd. 4#Air separation unit, is my 250,000 tons of methanol production lines of company
Corollary equipment, uses the KDON30000/24000 type air separation unit that Hangzhou Hangyang Joint-stock Co., Ltd produces, technological process
For molecular sieve purification Internal-compression flow, it is the our times most advanced technique of gas cryogenic separation, belongs to large air separation plant.For
Supporting 250,000 tons of methanol production oxygen nitrogen amounts, Hangzhou Hangyang Joint-stock Co., Ltd of device fabrication producer is our factory amount body manufacture,
By the novel oxygen generating plant designed and developed on the basis of Hang Yang producer in advance oxygen generating plant KDON28000 type oxygenerator.Wherein press
Power nitrogen 19500Nm3/ h design yield can meet my chemical company's whole production line pressure nitrogen gas amount demand.From 2009
Since this complete equipment operation in March in year, lower pressure tower nitrogen is unable to reach design yield always, and pressure nitrogen is taking 10000Nm3/h
Time cooling box temperature at 2 DEG C, pressure nitrogen gas gives user after low pressure heat exchanger heat exchange, when sending nitrogen quantity more than 10500Nm3/h
Time, pressure nitrogen gas cooling box temperature will gradually decrease to-17 DEG C with the increasing of taken amount, deviate former 23.5 DEG C～2 DEG C the most standing
Evaluation, even if when this covering device 70% load operation, pressure nitrogen gas taken amount in proportion should be at 13650Nm3Can only take during/h
10000Nm3The pressure nitrogen gas of/h.For avoiding low pressure heat exchanger is caused damage and the race of device is cold, pressure nitrogen gas taken amount one
Directly be in the state of low discharge, this operating mode affects vapor liquid equilibrium in tower, affect rectifying column in each section of reflux ratio, affect oxygen and produce
Amount.Pressure nitrogen gas taken amount deficiency need to additionally open two nitrogen compressors and supplement user's request amount, and pressure nitrogen gas does not reaches design load for a long time,
Have impact on space division normal rectification operating mode, hinder long-period stable operation, run counter to the original intention of high load capacity cost declining, constrain work
Factory's production capacity benefit development.
Summary of the invention
The problem that the present invention is directed to above-mentioned existence, affects air separation unit according to pressure tower nitrogen withdrawal amount under space division main distillation column and runs cold
The technical Analysis of factor, for pressure nitrogen gas taken amount deficiency problem, proposes solution: 1) the taking-up mouth of pipe is increased away from
Gas-liquid boiling section, reduces droplet entrainment；2) change singly take out mouth as black soy sauce mouth minimizing exit velocity into.Space division is reached after engineered
The stable adjustment of rectification operating mode, operational factor meets design load, reduces the tower fluctuation impact on ar system under main distillation column, disappears
Except low pressure heat exchanger low temperature stress fatigue and strength failure, add the purpose of the yield of pressure nitrogen gas.
The one of the present invention is applied to gas cryogenic separation equipment main distillation column, and it comprises rectifying column main body, two pressure nitrogen
Take out pipe, lower tower liquid nitrogen reflux pipe, low pressure heat exchanger, boiling section, heat exchanger and main condenser vaporizer in gas tower；Its
In, the gas outlet convergence taking out pipe in two described pressure nitrogen gas towers enters low pressure heat exchanger, two pressure nitrogen gas towers together
Interior taking-up pipe air inlet is respectively placed in top of tower under rectifying column main body；Described lower tower liquid nitrogen reflux pipe one end is with boiling section even
Logical, the other end connects with heat exchanger；Heat exchanger is positioned in main condenser vaporizer；Wherein, pipe is taken out in two pressure nitrogen gas towers
Mouth of pipe distance main condenser base of evaporator 50～60cm at the boiling section upper space of rectifying column main body.
The present invention comprises following beneficial effect:
The present invention is directed to air separation unit improve as follows: 1) the taking-up mouth of pipe is increased away from gas-liquid boiling section, eliminate drop
Carry secretly；2) change singly take out mouth as black soy sauce mouth minimizing exit velocity into.
Improved by above, bring following advantage:
(1) secure context
Take out the design of pipe by improving the height of pressure nitrogen conveying end and increasing in a pressure nitrogen gas tower, reduce taking-up
The flow velocity of gas, eliminates pressure nitrogen gas droplet entrainment phenomenon, it is to avoid cause low pressure heat exchanger and pipeline generation low temperature bursting by freezing harm
Major safety risks.
(2) economic benefit aspect
Having processed equipment fault, after pressure nitrogen gas normal supply, no longer underrun, has saved the energy, reduces power and disappears
Consumption, the development further for our factory provides guarantee.The basis of each column:
1, joint total value: 150.848 ten thousand yuan
Reduce by two nitrogen compressor operating costs:
250kwh × 0.29 × 2 × 8000h+22T/h × 0.15 × 2 × 8000h=150.848 ten thousand yuan
2, the new profit: 569.152 ten thousand yuan
New nitrogen pick-up yield 3000Nm3/h × 8000h × 0.3=720 ten thousand yuan
720-150.848=569.152 ten thousand yuan.
The mentality of designing of the present invention is as follows:
First, the present invention analyzes the low reason of pressure nitrogen gas temperature.Low pressure heat exchanger heat exchange is determined according to Calculation of Heat Transfer basic mode
The design of area calculates, and on another stock of low pressure heat exchanger, tower dirt nitrogen reflux gas outlet temperature meets design load 23.5 DEG C in addition, opinion
Demonstrate,proved this low pressure heat exchanger performance under design conditions no problem, eliminate the outer initiation pressure nitrogen temperature of rectifying column low because of
Element.
Secondly, the second factor is exactly that pressure nitrogen gas carrys out gas quality, and there is sieve plate liquid at the pressure nitrogen conveying end position that Xia Ta top is drawn
The drop that layer suspends and nitrogen together take out and are sent to low pressure heat exchanger, and the pressure nitrogen gas heat exchange containing drop is imitated by low pressure heat exchanger
Rate declines, and this is the main cause causing pressure nitrogen gas cooling box temperature low.Pressure nitrogen gas returns to design discharge to be needed to manage taking-up
Mouth position, mode are transformed, and first promote 1.04 meters of pressure nitrogen gas and take trachea height, simultaneously in 315 ° of main condenser vaporizer
Direction increases the pressure nitrogen fairlead of a DN300, and in parallel with original nitrogen pipeline, and two pipes take gas mode and reduce and take gas
Flow velocity is to reach to reduce the effect of droplet entrainment, and both processing modes have recovered pressure nitrogen gas nominal situation.
Owing to the pipeline majority in cold insulated cabinet is cryogenic liquid or cryogenic gas pipeline, but their temperature levels is the most different.For
Avoid unnecessary cold damage, when pipe arrangement it should be noted that following item as far as possible:
1) each pipeline must not be collided, and hot and cold tube should not lean on the nearest, and spacing should be greater than 100mm.Had better not be parallel to each other
Arrange；2) various liquid lines or cold pipe should be close proximity to internal cold containers, and gas piping is arranged in outside liquid line；
3) gas piping should be in following scope from the distance (namely heat insulation layer thickness) of cold insulation tank wall: when-50～-130 DEG C, Ying great
In 200～400mm；When-130～-196 DEG C, should be greater than 300～600mm；4) liquid discharge tube road should be specifically noted that
The cold damage preventing liquid from constantly gasifying and to increase.Fairlead is preferably inclined upwardly, and in the range of cold insulated cabinet about 800mm
Making bend pipe upwards, height is about 6～10 times of diameters, but cannot be less than 200mm.If there is irrational configuration,
Whole discharging tube has been filled with liquid, and raises due to temperature at cold insulated cabinet shell, and liquid in pipe will gasification.Bubble to
Upper motion can return again in container, continues again dirty with stylish liquid.So constantly come and go, in whole pipe, have liquid all the time
Constantly gasification, surrounding barrel shell temperature reduces, produces cold frost, even bursting by freezing cold insulation casing, and cold constantly loses.
Relatively reasonable disposition is one fluid-tight of formation when the valve is closed, and liquid will not constantly flow to the gasification of valve side.Have arranges liquid
Go out pipeline added with sleeve pipe of heating, with anti-freeze；5) in order to reduce the cold damage by pipeline and equipment supporter, should add during installation and lead
The asbestos pad of hot property difference.
At the existing liquid nitrogen in air separation column top, there is again gas nitrogen:, temperature when boiling water it will be seen that at atmosheric pressure
Being increased to 100 DEG C, water comes to life.But, water is not the most all to become steam, and is as absorbing heat,
Quantity of steam is continuously increased.In the stage that vapour, liquid coexist, it is " saturation ".Steam under this state " saturated vapor ",
Water is " saturation water ".At whole evaporation stage, steam and water have identical temperature, so being again " saturation temperature ".
The situation at rectifying column top is similar, and gas nitrogen and liquid nitrogen are in the saturation coexisted, and have identical saturated temperature
Degree.But, saturated liquid at identical temperature and saturated vapor belong to different states.Saturated vapor releases hot condensable one-tenth
Saturated liquid, temperature keeps constant, and this partial heat is referred to as " condensation latent heat "；It is saturated that saturated liquid absorbs hot annoying chemical conversion
Steam, temperature also maintains saturation temperature constant, and this partial heat is referred to as " evaporation latent heat ".To same material, identical
Pressure under, the two numerically equal.
Affect the factor of exchanger heat transfer capacity (thermic load): fluid is a complex mistake by the diabatic process of wall
Journey, the factor affecting heat output is a lot.Experiment shows, heat output Q hourly (being also thermic load) and cold and hot fluid
Temperature difference △ t (DEG C) is directly proportional, with heat transfer area F (m2) size be directly proportional, being write as formula is then
Q=3600KF △ t (kJ/h)
COEFFICIENT K in formula, heat transfer coefficient, represents when wall both sides fluid temperature difference is 1 DEG C by the heat transfer energy of unit are
Power, its unit is w/ (m2℃).Heat transfer coefficient reflect had an impact in addition to heat transfer area F and the temperature difference △ t heat transfer various
Factor.Obviously, energy saving is the biggest, represents that heat-transfer capability is the strongest.Otherwise it is the most weak.To what air separation unit was arranged
Various heat exchangers, its heat transfer area has determined that constant.
Relational language brief introduction of the present invention is as follows:
Rectifying column: rectifying column is also air separation column, when air rectification, nitrogen constantly escapes into gas from liquid, and oxygen
Constantly from gas, condense out entrance liquid.This process occurs when gas contacts with liquid.Rectifying column is a kind of
Strengthening device, it is by the effect of column plate, makes gas-liquid two-phase have sufficient attaching space, thus strengthens the friendship of heat and quality
Change, finally air is separated into oxygen and nitrogen.
Boiling: liquid surface and the violent vaporization phenomenon of internal generation, is named boiling.The region being in this situation is boiling section.
Reflux ratio: reflux ratio generally refers to down-flowing liquid amount in tower and the ratio rising vapor volume, and it is also called liquid-gas ratio.And
In Chemical Manufacture, reflux ratio generally refers to the ratio of down-flowing liquid amount and the overhead distillate scale of construction in tower.The purity of rectification product,
Under conditions of the number of plates is certain, depend on the size of reflux ratio.Gas phase nitrogen purity obtained when reflux ratio is big is high, liquid phase
Oxygen purity is the lowest.The gas phase nitrogen purity that reflux ratio hour obtains is low, and the oxygen purity of liquid phase is the highest.This is because temperature is higher
The down-flowing liquid rising gas relatively low with temperature mixes on column plate, after carrying out caloic exchange, and their temperature in the ideal case
Can reach unanimity, i.e. reach same temperature.This temperature is between original air-liquid temperature.If reflux ratio is big,
When the dirtiest cold liquid steam that is many or that rise is few, then gas-liquid mixed temperature is necessarily partial to cryogenic liquid, then goes up
The temperature drop rising steam is the biggest, and steam condenses the most.Because oxygen is difficult volatile component, therefore oxygen component condenses out the most more
A bit, the nitrogen concentration of the uprising gas so leaving column plate also improves soon.Every block of column plate is not always the case, and therefore obtains at tower top
The nitrogenous purity of gas just high.On the other hand, because gas-liquid mixed temperature is partial to cryogenic liquid, then down-flowing liquid
Temperature rise is the least, and liquid evaporates also few, thus the nitrogen component being evaporated in liquid is less, so leaves column plate
In down-flowing liquid, oxygen concentration just improves slowly.Every block of column plate is not always the case, thus the lowest at the oxygen concentration of the liquid obtained at the bottom of tower.
Reflux ratio hour is then contrary with above-mentioned situation, the adjustment of rectification operating mode, each position in actually mainly changing tower exactly
The size of reflux ratio.Rectifying tower temperature that operator often says is high, and actual to refer to reflux ratio little；Tower temperature is low, it is simply that return
The situation that flow ratio is big.
Pressure nitrogen gas: pressure nitrogen gas is tower upper product under main distillation column, takes out mouth through pressure nitrogen and takes out, through low pressure heat exchanger
It is continuously introduced into pipe network as product gas, for rear line production and application with after the just stream air heat-exchange after purification.
Accompanying drawing explanation
Fig. 1 is existing rectifying tower structure schematic diagram；
Fig. 2 is rectifying tower structure schematic diagram of the present invention.
Detailed description of the invention
Present invention is not limited only to the content of the respective embodiments described above, the combination of one of them or several detailed description of the invention with
Sample can also realize the purpose of invention.
Detailed description of the invention one: the one of present embodiment is applied to gas cryogenic separation equipment main distillation column, and it comprises rectification
Take out in 1, two pressure nitrogen gas towers of tower main body pipe 2,3, low pressure heat exchanger 4 of lower tower liquid nitrogen reflux pipe, boiling section 5,
Heat exchanger 6 and main condenser vaporizer 7；Wherein, the gas outlet taking out pipe 2 in two described pressure nitrogen gas towers is converged together
Enter low pressure heat exchanger 4, take out pipe 2 air inlet in two pressure nitrogen gas towers and be respectively placed in 1 time top of tower of rectifying column main body；
Described lower tower liquid nitrogen reflux pipe 3 one end connects with boiling section 5, and the other end connects with heat exchanger 6；Heat exchanger 6 is positioned at master
In condenser/evaporator 7；Wherein, the pipe 2 boiling section 5 upper space in rectifying column main body 1 is taken out in two pressure nitrogen gas towers
The mouth of pipe distance main condenser vaporizer 7 bottom 50～60cm.
Detailed description of the invention two: present embodiment is unlike detailed description of the invention one: in two described pressure nitrogen gas towers
Take out pipe 2 and lay respectively at 1 time top of tower both sides of rectifying column main body.Other is identical with detailed description of the invention one.
By following example checking beneficial effects of the present invention:
Embodiment one
In conjunction with Fig. 2, the structure of the present embodiment is illustrated:
The present embodiment be applied to gas cryogenic separation equipment main distillation column, it comprises 1, two pressure nitrogen gas of rectifying column main body
Pipe 2,3, low pressure heat exchanger 4 of lower tower liquid nitrogen reflux pipe, boiling section 5, heat exchanger 6 and main condenser evaporation is taken out in tower
Device 7；Wherein, in two described pressure nitrogen gas towers, the gas outlet of taking-up pipe 2 is converged and is entered low pressure heat exchanger 4 together, and two
Take out pipe 2 air inlet in individual pressure nitrogen gas tower and be respectively placed in boiling section 5 upper space of rectifying column main body 1；Described lower tower
Liquid nitrogen reflux pipe 3 one end connects with boiling section 5, and the other end connects with heat exchanger 6；Heat exchanger 6 is positioned at main condenser vaporizer
In 7；Wherein, the pipe 2 mouth of pipe height at boiling section 5 upper space of rectifying column main body 1 is taken out in two pressure nitrogen gas towers
It is on original height, increase 1.04 meters.
The present embodiment is centering coal dragonization Harbin aqueous vapor subsidiary factory of Coal Chemical Industry company limited 4#Air separation unit is by Hangzhoupro, Hangzhou oxygen stock
The KDON30000/24000 type air separation unit that part company limited produces, through cut gas, heat, replace, take off sand, measurement,
Draw, improved, according to modification scheme to space division rectifying column king-tower mouthpiece, promote 1.04 meters of pressure nitrogen gas and take gas
Pipe height, increases the pressure nitrogen fairlead of a DN300 in 315 ° of directions of main condenser vaporizer, and two kinds of measures reach to subtract
The purpose of few droplet entrainment.In the case of not having experience more there is no industrialized production demonstration plant, successfully complete
Transformation in KDON30000/24000 large-scale space division device tower, transformation data and scientific research technology have promotion price in the same industry
Value.
Before the present embodiment transformation, air separation unit can only send about 13500 pressure nitrogen gas to can not meet the need of gas making, purification, methanol
Want, send to meet after technological requirement must open two nitrogen compressor force feeds, annual waste substantial amounts of water, electricity.After transformation
In actual motion, reaching the supply of air separation unit complete independently pressure nitrogen gas, flow reaches 19000, stable conditions.Transformation is saved
The investments such as equipment, technology, occupation of land, it is achieved reduce the purpose of production cost energy efficient.Run good from transforming equipment so far
Good.This transform innovation transformation as, and technique is promoted by existing Hangzhoupro oxygen, is widely used in more than 30,000 air separation units,
Aspect of saving energy and reduce the cost in space division field has good development prospect.
Claims (2)
1. one kind is applied to gas cryogenic separation equipment main distillation column, it is characterised in that it comprise rectifying column main body (1), two
Take out pipe (2), lower tower liquid nitrogen reflux pipe (3), low pressure heat exchanger (4), a boiling section (5) in pressure nitrogen gas tower, change
Hot device (6) and main condenser vaporizer (7)；Wherein, the gas outlet taking out pipe (2) in two described pressure nitrogen gas towers is converged
The poly-low pressure heat exchanger (4) that enters together, takes out pipe (2) air inlet and is respectively placed in rectifying column main body (1) in two pressure nitrogen gas towers
Lower top of tower；Described lower tower liquid nitrogen reflux pipe (3) one end connects with boiling section (5), and the other end is with heat exchanger (6) even
Logical；Heat exchanger (6) is positioned in main condenser vaporizer (7)；Wherein, pipe (2) is taken out in two pressure nitrogen gas towers in rectification
Mouth of pipe distance main condenser vaporizer (7) bottom 50～60cm of boiling section (5) upper space of tower main body (1).
One the most according to claim 1 is applied to gas cryogenic separation equipment main distillation column, it is characterised in that described
Take out pipe (2) in two pressure nitrogen gas towers and lay respectively at top of tower both sides under rectifying column main body (1).
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| CN201510001527.0A CN104534812B (en) | 2015-01-04 | 2015-01-04 | One is applied to gas cryogenic separation equipment main distillation column |
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| CN104534812B true CN104534812B (en) | 2016-10-19 |
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Citations (6)
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|---|---|---|---|---|
| CN1044850A (en) * | 1984-07-13 | 1990-08-22 | 大同酸素株式会社 | Produce the device of high-purity nitrogen |
| US5740683A (en) * | 1997-03-27 | 1998-04-21 | Praxair Technology, Inc. | Cryogenic rectification regenerator system |
| EP0745817B1 (en) * | 1995-06-01 | 2001-09-26 | Air Water Inc. | oxygen gas manufacturing apparatus |
| CN1764813A (en) * | 2003-03-26 | 2006-04-26 | 空气及水株式会社 | Air separator |
| CN203980791U (en) * | 2014-06-09 | 2014-12-03 | 杭州杭氧股份有限公司 | A kind of device of producing nitrogen product with pressure |
| CN204373314U (en) * | 2015-01-04 | 2015-06-03 | 中煤能源黑龙江煤化工有限公司 | One is applied to gas cryogenic separation equipment main distillation column |
-
2015
- 2015-01-04 CN CN201510001527.0A patent/CN104534812B/en not_active Expired - Fee Related
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1044850A (en) * | 1984-07-13 | 1990-08-22 | 大同酸素株式会社 | Produce the device of high-purity nitrogen |
| EP0745817B1 (en) * | 1995-06-01 | 2001-09-26 | Air Water Inc. | oxygen gas manufacturing apparatus |
| US5740683A (en) * | 1997-03-27 | 1998-04-21 | Praxair Technology, Inc. | Cryogenic rectification regenerator system |
| CN1764813A (en) * | 2003-03-26 | 2006-04-26 | 空气及水株式会社 | Air separator |
| CN203980791U (en) * | 2014-06-09 | 2014-12-03 | 杭州杭氧股份有限公司 | A kind of device of producing nitrogen product with pressure |
| CN204373314U (en) * | 2015-01-04 | 2015-06-03 | 中煤能源黑龙江煤化工有限公司 | One is applied to gas cryogenic separation equipment main distillation column |
Non-Patent Citations (1)
| Title |
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| 富氧液空冷凝蒸发器的安全设计;范燕萍;《深冷技术》;20090228;全文 * |
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